US3594444A - Process for separating hydrocarbons and hydrogen fluoride catalyst from the effluent of an isoparaffin-olefin alkylation reaction zone - Google Patents

Process for separating hydrocarbons and hydrogen fluoride catalyst from the effluent of an isoparaffin-olefin alkylation reaction zone Download PDF

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US3594444A
US3594444A US831618A US3594444DA US3594444A US 3594444 A US3594444 A US 3594444A US 831618 A US831618 A US 831618A US 3594444D A US3594444D A US 3594444DA US 3594444 A US3594444 A US 3594444A
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hydrogen fluoride
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hydrocarbon
alkylation reaction
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Universal Oil Products Co
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/56—Addition to acyclic hydrocarbons
    • C07C2/58—Catalytic processes
    • C07C2/62—Catalytic processes with acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/06—Halogens; Compounds thereof
    • C07C2527/08—Halides
    • C07C2527/12—Fluorides
    • C07C2527/1206—Hydrogen fluoride

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  • the invention relates to a process for separating hydrocarbons and hydrogen fluoride catalyst. It particularly relates to a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoridehydrocarbon eflluent of an isoparafiin-olefin alkylation reaction zone.
  • catalytic alkylation utilizing sulfuric acid or hydrofluoric acid as the catalyst is an important chemical tool for preparing alkylated hydrocanbons and derivatives thereof.
  • the commercial and industrial demand for these products is exemplified by the demand for isoparaffin hydrocarbons and alkylsubstituted benzenes of the gasoline boiling range and with the demand for alkyl-substituted aromatics suitable for conversion for surfactants, e.g., detergents, wetting agents, and the like.
  • the catalytic alkylation process to which the present invention is especially applicable consists of a process in which a mixture of hydrocarbons containing isoparaffins such as isobutane, isopentane, and the like, and olefins such as propylene, butylenes, isobutene, amylenes, and the like, are mixed intimately in the presence of a strong acid catalyst such as hydrofluoric acid for a time sufficient to complete the reaction.
  • a strong acid catalyst such as hydrofluoric acid for a time sufficient to complete the reaction.
  • the eflluent from the reaction zone contains isoparaffin hydrocarbons of higher molecular weight than the isoparafiins in the original mixture. Isobutane has been used almost exclusively because of its reactivity and availability to produce high quality alkylate products.
  • alkylate as used in the specification and claims is intended to embody the higher molecular Weight reaction product from the alkylation reaction.
  • tbutenes have been used almost exclusively.
  • the present invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon eflluent of an isoparafiin-olefin alkylation reaction zone which comprises the steps of: (a) introducing the total hydrogen fluoride-hydrocarbon eflluent from said reaction zone into an upper portion of a first separation zone maintained under separation conditions suflicient to separate said hydrogen fluoride catalyst from the hydrocarbon portion of said effluent; (b) withdrawing settled hydrogen fluoride catalyst from an intermediate portion of said first separation zone as an intermediate fraction; (0) partially condensing a hereinafter specified first vapor fraction in external heat exchanger means wherein the hydrocarbon portion of step (a) is withdrawn from said first separation zone, indirectly heat exchanged with said first vapor fraction, and returned directly to said first separation zone at a locus below the locus for withdrawing said first vapor fraction; (d) withdrawing a first vapor fraction comprising propane and isoparaflinic hydrocarbons at a
  • the essence of my invention comprises utilizing a vapor fraction comprising propane and isoparafiin hydrocarbon that is partially condensed in an external heat exchanger zone utilizing the hydrocarbon portion of the efliuent that has been separated in the first separation zone as the medium for indirect heat exchange and, in conjunction with this feature, the desired alkylate product fraction is passed Without intervening cooling to a second separation zone reboiler means as the sole source of heat to this reboiler prior to subsequent recovery of the alkylate.
  • the total hydrogen fluoride-hydrocarbon eifiuent from an isop arafiin-olefin alkylation reaction zone (not shown) is introduced via line 1 into first separation zone 2 which is maintained under separation conditions sufficient to separate hydrogen fluoride catalyst from the hydrocarbon portion of the effluent.
  • the first separation zone has contacting means 3 such as perforated plates, trays, baflies and the like disposed above horizontal partition 4.
  • Horizontal partition 4 has weir means 5 extending downwardly from the partition to form vertical fluid passageway 6 between the upper and upper intermediate portions of the first separation zone.
  • the numeral 7 represents a second horizontal partition upon which the settled hydrogen fluoride remains until it is withdrawn from the intermediate portion of the first separation zone via line 8 as an intermediate fraction.
  • the hydrocarbon portion of the total efliuent is withdrawn from the first separation zone via line 10 and passed to external heat exchanger means 11 and returned directly to the first separation zone via line 12 at a locus below the locus for withdrawing a hereinafter described first vapor fraction.
  • the first vapor fraction comprises propane and isoparaflin hydrocarbons and is Withdrawn from the first separation zone via line 13 at a locus below the locus for withdrawing the settled hydrogen fluoride catalyst via line 8.
  • Normal parafiinic hydrocarbon is withdrawn, preferably, from a lower portion of the first separation zone, and is represented by the numeral 9.
  • the first separation zone has reboiler means 14 located in a bottom portion of the first separation zone and is disposed in well 15.
  • a hot oil system represented by the numeral 16 supplies heat to this separation zone.
  • Alkylated hydrocarbons are withdrawn without intervening cooling via line 17 from a bottoms portion of the first separation zone and are passed to reboiler means 18 positioned in a lower portion of the second separation zone 19 as the sole source of heat supplied to reboiler means 18.
  • Reboiler means 18 is disposed in well 20 with fluid passageway 21 formed by weir means 22 and well 20.
  • the housing contains a vapor riser means 23 communicating with an intermediate portion of said housing and is formed by means 22 and the housing of the second separation zone.
  • the partially condensed vapor fraction comprising propane and isoparaflinic hydrocarbons is introduced, in a preferred embodiment, via line 13 and cooler 13a into a bottom portion of second separation zone 19.
  • the second separation zone makes the separation between the isoparaflinic hydrocarbon, propane and any dissolved hydrogen fluoride.
  • Isoparaffinic hydrocarbon is withdrawn from a bottom portion of second separation zone 19 via line 40, passed through cooler 41 through line 42 via pump 43 and line 44 to provide, in a preferred mode of operation, isoparafiinic hydrocarbon recycle to the alkylation reaction zone.
  • the propane and hydrogen fluoride passes upwardly in second separation zone 19 through vapor riser 26 which is formed by horizontal partition means 24 and weir means 25 into an upper section of the second separation zone.
  • Coolant via line is supplied to cooling means 36 and a propane-containing stream is removed from the second separation zone via line 29 and passed to external stripping means 30 which has disposed therein reboiler 31 supplied by steam means 32.
  • At least a portion of the propane is removed from stripping zone 30 via line 33 and the remainder along with hydrogen fluoride is recycled back to the second separation zone from stripping means 30 via line 34.
  • hydrogen fluoride catalyst may be withdrawn via line 28 from the second separation zone for recycle to the isoparaflin-olefin alkylation reaction zone.
  • Vent gas if any, may be removed from the upper portion of the second separation zone.
  • Reflux comprising propane and dissolved hydrogen fluoride is refluxed from an upper portion of the second separation zone by liquid downcomer means 27.
  • the desired alkylate fraction that was passed to reboiler means 18 by line 17 is recovered and sent to storage via line 37, cooler 38 and line 39.
  • the first separation zone operates so that the zone formed above horizontal partition means 4 is a settling zone to take advantage of the fact that the hydrogen fluoride alkylation catalyst is heavier than the hydrocarbon portion of the effluent so that the catalyst gravitates downwardly to partition 7 for removal via line 8 from the first separation zone.
  • the remaining hydrocarbon containing only dissolved hydrogen fluoride passes via lines 10 and 12 into a lower portion of the first separation zone where the hydrocarbon is heated by reboiler 14. Normal butane vapors leave the separation zone via line 9 as a side-cut fraction and the desired heavier alkylate is removed via line 17.
  • the vapors from the stripping section of the first separation zone then pass via line 13 and cooler 13a to the second separation zone where propane is separated from the isoparaflinic hydrocarbon.
  • the propane and hydrogen fluoride vapors pass through vapor riser means 26 and are condensed by a water or refrigerated exchanger 36.
  • the condensed hydrogen fluoride is gravitated into an acid settler section and removed via line 28 above partition 24.
  • the propane is stripped of hydrogen fluoride in stripper means 30 and is then pressured to storage via line 33. A portion of the propane is recycled back into the second separation zone as reflux.
  • the isoparaflinic hydrocarbon is separated as a liquid bottoms product and in a preferred embodiment is passed to the alkylation reactor.
  • this invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon etfiuent of an isobutane-butene alkylation reaction zone which comprises the steps of: (a) introducing the total hydrogen fluoride-hydrocarbon effluent from said reaction zone into an upper portion of a first separation zone maintained under separation conditions sufficient to separate said hydrogen fluoride catalyst from the hydrocarbon portion of said etfluent; (b) Withdrawing settled hydrogen fluoride catalyst from an intermediate portion of said first separation zone as an intermediate fraction; (c) partially condensing a hereinafter specified first vapor fraction in external heat exchanger means wherein the hydrocarbon portion of step (a) is withdrawn from said first separation zone, indirectly heat exchanged with said first vapor fraction, and returned directly to said first separation zone at a locus below the locus for withdrawing said first vapor fraction; ((1) withdrawing a first vapor fraction comprising propane
  • the present invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon efliuent of an isoparaffin-olefin alkylation reaction zone utilizing a simplified processing scheme and a more economical and eflicient piping and heating system than previous prior art design.
  • a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon eflluent of an isoparaflin-olefin alkylation reaction zone which comprises the steps of:
  • a separation zone superjacent to a hereinafter specified stripping zone, into a hydrogen fluoride phase and a hydrocarbon phase containing dissolved hydrogen fluoride;
  • step (g) partially condensing said vapor fraction by said indirect heat exchange with said hydrocarbon phase according to step (b);
  • step (h) passing said partially condensed fraction of step (g) as feed to a fractionation zone maintained under fractionation conditions sufiicient to provide an overhead stream comprising propane and hydrogen fluoride and a bottoms stream comprising isoparaifinic hydrocarbons;
  • step (i) supplying the total amount of reboiling heat required for said fractionation zone to the lower portion thereof by indirect exchange with said alkylate fraction of step (e);
  • step (h) is passed to a second stripper zone wherein hydrogen fluoride is stripped from said propane.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

PROCESS FOR SEPARATING HYDROCARBONS AND HYDROGEN FLUORIDE CATALYST FROM THE TOTAL HYDROGEN FLUORIDE-HYDROCARBON EFFLUENT OF AN ISOPARAFFIN-OLEFIN ALKYLATION REACTION ZONE IN A PROCESSING SYSTEM WHEREIN A VAPOR FRACTION COMPRISING PROPANE AND ISOPARAFFINIC HYDROCARBONS IS PARTIALLY CONDENSED IN AN EXTERNAL HEAT EXCHANGER MEANS UTILIZING HYDROCARBON SEPARATED IN A FIRST SEPARATION ZONE AS

THE MEDIUM FOR INDIRECT HEAT EXCHANGE AND WHEREIN THE DESIRED ALKYLATED FRACTION IS PASSED TO SECOND SEPARATION ZONE REBOILER MEANS AS THE SOLE SOURCE OF HEAT TO THIS REBOILER PRIOR TO RECOVERY.

Description

Goo/am July 20, 1971 E. K. JONES 3,594,444
PROCESS FOR SEPARATING HYDROCARBONS AND HYDROGEN FLUORIDE CATALYST FROM THE EFFLUENT OF AN ISOPARAFFIN-OLEFIN ALKYLATION REACTION ZONE Filed June 9, 1969 J A/ky/afe f0 .S'forage l/enf Gas HF f0 Reactor 'Q Q Q m U S h a m K I HF r0 Reactor /s0bu/ane to Race S u E Q:
//Vl/E/VTOR.- Edwin K, Jones United States Patent O 3,594,444 PROCESS FOR SEPARATHN G HYDROQARBONS AND HYDROGEN FLUORIDE CATALYST FROM THE EFFLUENT OF AN ISOPARAFFIN- OLEFIN ALKYLATION REACTION ZONE Edwin K. Jones, Kenilworth, 111., assignor to Universal Oil Products Company, Des Plaines, Ill. Filed June 9, 1969, Ser. No. 831,618 Int. Cl. C07c 3/54; B0111 3/00 U.S. Cl. 260-68348 6 Claims ABSTRACT OF THE DISCLOSURE BACKGROUND OF THE INVENTION The invention relates to a process for separating hydrocarbons and hydrogen fluoride catalyst. It particularly relates to a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoridehydrocarbon eflluent of an isoparafiin-olefin alkylation reaction zone.
It is well known in the prior art that catalytic alkylation utilizing sulfuric acid or hydrofluoric acid as the catalyst is an important chemical tool for preparing alkylated hydrocanbons and derivatives thereof. The commercial and industrial demand for these products is exemplified by the demand for isoparaffin hydrocarbons and alkylsubstituted benzenes of the gasoline boiling range and with the demand for alkyl-substituted aromatics suitable for conversion for surfactants, e.g., detergents, wetting agents, and the like.
The catalytic alkylation process to which the present invention is especially applicable consists of a process in which a mixture of hydrocarbons containing isoparaffins such as isobutane, isopentane, and the like, and olefins such as propylene, butylenes, isobutene, amylenes, and the like, are mixed intimately in the presence of a strong acid catalyst such as hydrofluoric acid for a time sufficient to complete the reaction. The eflluent from the reaction zone contains isoparaffin hydrocarbons of higher molecular weight than the isoparafiins in the original mixture. Isobutane has been used almost exclusively because of its reactivity and availability to produce high quality alkylate products. Accordingly, for convenience, the term alkylate as used in the specification and claims is intended to embody the higher molecular Weight reaction product from the alkylation reaction. In similar manner among the olefins, tbutenes have been used almost exclusively. Propylene and the pentents, and even higher boiling olefinic hydrocarbons, can be used according to their availability.
SUMMARY OF THE INVENTION carbon efiluent of an isopraffin-olefin alkylation reaction zone. a
3,594,444 Patented July 20, 1971 It is another object of this invention to provide a separation process in a more facile, economical and efficient manner in a particular environment which has presented peculiar and difficult problems.
Therefore, the present invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon eflluent of an isoparafiin-olefin alkylation reaction zone which comprises the steps of: (a) introducing the total hydrogen fluoride-hydrocarbon eflluent from said reaction zone into an upper portion of a first separation zone maintained under separation conditions suflicient to separate said hydrogen fluoride catalyst from the hydrocarbon portion of said effluent; (b) withdrawing settled hydrogen fluoride catalyst from an intermediate portion of said first separation zone as an intermediate fraction; (0) partially condensing a hereinafter specified first vapor fraction in external heat exchanger means wherein the hydrocarbon portion of step (a) is withdrawn from said first separation zone, indirectly heat exchanged with said first vapor fraction, and returned directly to said first separation zone at a locus below the locus for withdrawing said first vapor fraction; (d) withdrawing a first vapor fraction comprising propane and isoparaflinic hydrocarbons at a locus below the locus for withdrawing said settled hydrogen fluoride catalyst; (e) Withdrawing normal parafiinic hydrocarbon from said first separation zone; (f) withdrawing without intervening cooling alkylated hydrocarbons from a bottoms portion of said first separation zone as an alkylate fraction; (g) introducing said partially condensed fraction of step (c) into a second separation zone and passing said alkylate fraction of step (f) to reboiler means positioned in a lower portion of said second separation zone as the sole source of heat supplied to said reboiler means; (h) withdrawing isoparaifinic hydrocarbon from a bottom portion of said second separation zone and a propanecontaining stream from an upper portion of said zone; and, (i) recovering the alkylate fraction passed to said reboiler means of step (g).
As will be described hereinafter in greater detail, the essence of my invention comprises utilizing a vapor fraction comprising propane and isoparafiin hydrocarbon that is partially condensed in an external heat exchanger zone utilizing the hydrocarbon portion of the efliuent that has been separated in the first separation zone as the medium for indirect heat exchange and, in conjunction with this feature, the desired alkylate product fraction is passed Without intervening cooling to a second separation zone reboiler means as the sole source of heat to this reboiler prior to subsequent recovery of the alkylate.
My invention can be more clearly described and illustrated with reference to the attached drawing which is a schematic representation of a preferred embodiment of my invention.
DESCRIPTION OF THE DRAWING Referring now to the drawing, the total hydrogen fluoride-hydrocarbon eifiuent from an isop arafiin-olefin alkylation reaction zone (not shown) is introduced via line 1 into first separation zone 2 which is maintained under separation conditions sufficient to separate hydrogen fluoride catalyst from the hydrocarbon portion of the effluent. In a preferred embodiment, the first separation zone has contacting means 3 such as perforated plates, trays, baflies and the like disposed above horizontal partition 4. Horizontal partition 4 has weir means 5 extending downwardly from the partition to form vertical fluid passageway 6 between the upper and upper intermediate portions of the first separation zone. In the drawing, the numeral 7 represents a second horizontal partition upon which the settled hydrogen fluoride remains until it is withdrawn from the intermediate portion of the first separation zone via line 8 as an intermediate fraction.
The hydrocarbon portion of the total efliuent is withdrawn from the first separation zone via line 10 and passed to external heat exchanger means 11 and returned directly to the first separation zone via line 12 at a locus below the locus for withdrawing a hereinafter described first vapor fraction. The first vapor fraction comprises propane and isoparaflin hydrocarbons and is Withdrawn from the first separation zone via line 13 at a locus below the locus for withdrawing the settled hydrogen fluoride catalyst via line 8.
Normal parafiinic hydrocarbon is withdrawn, preferably, from a lower portion of the first separation zone, and is represented by the numeral 9.
The first separation zone has reboiler means 14 located in a bottom portion of the first separation zone and is disposed in well 15. A hot oil system represented by the numeral 16 supplies heat to this separation zone.
Alkylated hydrocarbons are withdrawn without intervening cooling via line 17 from a bottoms portion of the first separation zone and are passed to reboiler means 18 positioned in a lower portion of the second separation zone 19 as the sole source of heat supplied to reboiler means 18. Reboiler means 18 is disposed in well 20 with fluid passageway 21 formed by weir means 22 and well 20. The housing contains a vapor riser means 23 communicating with an intermediate portion of said housing and is formed by means 22 and the housing of the second separation zone.
The partially condensed vapor fraction comprising propane and isoparaflinic hydrocarbons is introduced, in a preferred embodiment, via line 13 and cooler 13a into a bottom portion of second separation zone 19.
The second separation zone makes the separation between the isoparaflinic hydrocarbon, propane and any dissolved hydrogen fluoride. Isoparaffinic hydrocarbon is withdrawn from a bottom portion of second separation zone 19 via line 40, passed through cooler 41 through line 42 via pump 43 and line 44 to provide, in a preferred mode of operation, isoparafiinic hydrocarbon recycle to the alkylation reaction zone.
The propane and hydrogen fluoride passes upwardly in second separation zone 19 through vapor riser 26 which is formed by horizontal partition means 24 and weir means 25 into an upper section of the second separation zone. Coolant via line is supplied to cooling means 36 and a propane-containing stream is removed from the second separation zone via line 29 and passed to external stripping means 30 which has disposed therein reboiler 31 supplied by steam means 32. At least a portion of the propane is removed from stripping zone 30 via line 33 and the remainder along with hydrogen fluoride is recycled back to the second separation zone from stripping means 30 via line 34.
In a preferred embodiment, hydrogen fluoride catalyst may be withdrawn via line 28 from the second separation zone for recycle to the isoparaflin-olefin alkylation reaction zone. Vent gas, if any, may be removed from the upper portion of the second separation zone. Reflux comprising propane and dissolved hydrogen fluoride is refluxed from an upper portion of the second separation zone by liquid downcomer means 27.
The desired alkylate fraction that was passed to reboiler means 18 by line 17 is recovered and sent to storage via line 37, cooler 38 and line 39.
As will be understood by one skilled in the art, the first separation zone operates so that the zone formed above horizontal partition means 4 is a settling zone to take advantage of the fact that the hydrogen fluoride alkylation catalyst is heavier than the hydrocarbon portion of the effluent so that the catalyst gravitates downwardly to partition 7 for removal via line 8 from the first separation zone. The remaining hydrocarbon containing only dissolved hydrogen fluoride passes via lines 10 and 12 into a lower portion of the first separation zone where the hydrocarbon is heated by reboiler 14. Normal butane vapors leave the separation zone via line 9 as a side-cut fraction and the desired heavier alkylate is removed via line 17. The vapors from the stripping section of the first separation zone then pass via line 13 and cooler 13a to the second separation zone where propane is separated from the isoparaflinic hydrocarbon. In the second separation zone, the propane and hydrogen fluoride vapors pass through vapor riser means 26 and are condensed by a water or refrigerated exchanger 36. The condensed hydrogen fluoride is gravitated into an acid settler section and removed via line 28 above partition 24. The propane is stripped of hydrogen fluoride in stripper means 30 and is then pressured to storage via line 33. A portion of the propane is recycled back into the second separation zone as reflux. The isoparaflinic hydrocarbon is separated as a liquid bottoms product and in a preferred embodiment is passed to the alkylation reactor.
PREFERRED EMBODIMENT In a particularly preferred embodiment of my invention, this invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon etfiuent of an isobutane-butene alkylation reaction zone which comprises the steps of: (a) introducing the total hydrogen fluoride-hydrocarbon effluent from said reaction zone into an upper portion of a first separation zone maintained under separation conditions sufficient to separate said hydrogen fluoride catalyst from the hydrocarbon portion of said etfluent; (b) Withdrawing settled hydrogen fluoride catalyst from an intermediate portion of said first separation zone as an intermediate fraction; (c) partially condensing a hereinafter specified first vapor fraction in external heat exchanger means wherein the hydrocarbon portion of step (a) is withdrawn from said first separation zone, indirectly heat exchanged with said first vapor fraction, and returned directly to said first separation zone at a locus below the locus for withdrawing said first vapor fraction; ((1) withdrawing a first vapor fraction comprising propane and isobutane at a locus below the locus for withdrawing said settled hydrogen fluoride catalyst; (e) withdrawing normal butane from a lower portion of said first separation zone; (1?) withdrawing, without intervening cooling, alkylated hydrocarbons from a bottoms portion of said first separation zone as an alkylate fraction; (g) introducing said partially condensed fraction of step (0) into a second separation zone and passing said alkylate fraction of step (f) to reboiler means positioned in a lower portion of said second separation zone as the sole source of heat supplied to said reboiler means; (h) withdrawing isobutane from a bottom portion of said second separation zone and a propane-containing stream from an upper portion of said zone; (i) passing said propane-containing stream to an external stripping zone wherein hydrogen fluoride is separated from said propane and recycled to said second separation zone; (j) withdrawing hydrogen fluoride from said second separation zone for recycle to said isobutane-butene alkylation reaction zone; and, (k) recovering the alkylate fraction passed to said reboiler means of step (g).
It is apparent that the present invention provides a process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon efliuent of an isoparaffin-olefin alkylation reaction zone utilizing a simplified processing scheme and a more economical and eflicient piping and heating system than previous prior art design.
I claim as my invention:
1. A process for separating hydrocarbons and hydrogen fluoride catalyst from the total hydrogen fluoride-hydrocarbon eflluent of an isoparaflin-olefin alkylation reaction zone which comprises the steps of:
(a) separating said total effluent by gravity settling, in
a separation zone superjacent to a hereinafter specified stripping zone, into a hydrogen fluoride phase and a hydrocarbon phase containing dissolved hydrogen fluoride;
(b) heating said hydrocarbon phase by indirect heat exchange with a hereinafter specified vapor fraction;
(c) introducing the resulting heated hydrocarbon phase as feed to the upper portion of a stripping zone;
(d) supplying reboiling heat to the lower portion of said stripping zone;
(e) withdrawing an alkylate fraction comprising alkylated hydrocarbons from the bottom portion of said stripping zone and passing said alkylate fraction, without intervening cooling, to the lower portion of a hereinafter specified fractionation zone as the reboiler heating medium therefor; 1
(f) withdrawing a vapor fraction comprising propane, isoparaffinic hydrocarbons and hydrogen fluoride from said stripping. zone at a locus above the feed locus;
(g) partially condensing said vapor fraction by said indirect heat exchange with said hydrocarbon phase according to step (b);
(h) passing said partially condensed fraction of step (g) as feed to a fractionation zone maintained under fractionation conditions sufiicient to provide an overhead stream comprising propane and hydrogen fluoride and a bottoms stream comprising isoparaifinic hydrocarbons;
(i) supplying the total amount of reboiling heat required for said fractionation zone to the lower portion thereof by indirect exchange with said alkylate fraction of step (e); and
(j)recovering said alkylate fraction after abstracting heat therefrom according to step (i).
2. The process according to claim 1 wherein said isoparaffin-olefin alkylation reaction zone is processing iso butane and an olefin having from 3 to 5 carbon atoms per molecule.
3. The process according to claim 1 wherein said isoparaflin-olefin alkylation reaction zone is processing isobutane and a butene.
4. The process according to claim 1 wherein said settled hydrogen fluoride catalyst of step (a) is recycled to the isoparaffin-olefin alkylation reaction zone.
5. The process according to claim 1 wherein said isoparafiinic hydrocarbon of step (h) is recycled to the isoparafiin-olefin alkylation reaction zone.
6. The process according to claim 1 wherein said propane overhead stream of step (h) is passed to a second stripper zone wherein hydrogen fluoride is stripped from said propane.
' References Cited UNITED STATES PATENTS 3,073,877 1/1963 Sherk 260683.48 3,254,137 5/1966 Hutto et a1 260683.48 3,370,003 2/1968 Borst, Jr 260683.62 3,402,123 9/1968 Coste 260683.62 3,431,079 3/1969 Chapman 260683.48
DELBERT E. GANTZ, Primary Examiner G. J. CRASANAKIS, Assistant Examiner US. Cl. X.R.
US831618A 1969-06-09 1969-06-09 Process for separating hydrocarbons and hydrogen fluoride catalyst from the effluent of an isoparaffin-olefin alkylation reaction zone Expired - Lifetime US3594444A (en)

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3920767A (en) * 1974-05-29 1975-11-18 Phillips Petroleum Co Isoparaffin-olefin alkylation using hf-ethyl fluoride catalysis with recovery of ethyl fluorine and alkylation of secondary and tertiary alkyl fluorides
US3957901A (en) * 1972-07-28 1976-05-18 Phillips Petroleum Company Indirect heat exchange in alkylation
US3993706A (en) * 1975-10-28 1976-11-23 Uop Inc. Acid purification and recycle in HF-catalyzed alkylation
US4144281A (en) * 1978-04-27 1979-03-13 Phillips Petroleum Company HF Alkylation process utilizing compressed isoparaffin vapor in indirect heat exchanges
US4182925A (en) * 1973-12-12 1980-01-08 Phillips Petroleum Company Alkylation effluent recovery system
US4777323A (en) * 1985-07-19 1988-10-11 Phillips Petroleum Company Catalytic alkylation process

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3957901A (en) * 1972-07-28 1976-05-18 Phillips Petroleum Company Indirect heat exchange in alkylation
US4182925A (en) * 1973-12-12 1980-01-08 Phillips Petroleum Company Alkylation effluent recovery system
US3920767A (en) * 1974-05-29 1975-11-18 Phillips Petroleum Co Isoparaffin-olefin alkylation using hf-ethyl fluoride catalysis with recovery of ethyl fluorine and alkylation of secondary and tertiary alkyl fluorides
US3993706A (en) * 1975-10-28 1976-11-23 Uop Inc. Acid purification and recycle in HF-catalyzed alkylation
US4144281A (en) * 1978-04-27 1979-03-13 Phillips Petroleum Company HF Alkylation process utilizing compressed isoparaffin vapor in indirect heat exchanges
US4777323A (en) * 1985-07-19 1988-10-11 Phillips Petroleum Company Catalytic alkylation process

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